EP1946829A1 - Procédé et appareil pour le traitement des déchets - Google Patents

Procédé et appareil pour le traitement des déchets Download PDF

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Publication number
EP1946829A1
EP1946829A1 EP07000166A EP07000166A EP1946829A1 EP 1946829 A1 EP1946829 A1 EP 1946829A1 EP 07000166 A EP07000166 A EP 07000166A EP 07000166 A EP07000166 A EP 07000166A EP 1946829 A1 EP1946829 A1 EP 1946829A1
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EP
European Patent Office
Prior art keywords
vessel
steam
waste
process according
air
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP07000166A
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German (de)
English (en)
Inventor
John Duncan Grierson
Philip James Campion
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sterecycle Ltd
Original Assignee
Sterecycle Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sterecycle Ltd filed Critical Sterecycle Ltd
Priority to EP07000166A priority Critical patent/EP1946829A1/fr
Priority to TW96149627A priority patent/TW200918192A/zh
Priority to US12/522,191 priority patent/US20100160709A1/en
Priority to GB0902385A priority patent/GB2456074B/en
Priority to GB0800071A priority patent/GB2445466B/en
Priority to GB0800073A priority patent/GB2445467B/en
Priority to PCT/EP2008/050041 priority patent/WO2008081028A2/fr
Priority to CL2008000013A priority patent/CL2008000013A1/es
Priority to GB0800074A priority patent/GB2445468B/en
Priority to EP20080701223 priority patent/EP2107935A2/fr
Priority to GB0800045A priority patent/GB2445465B/en
Priority to GB0800072A priority patent/GB2448390A/en
Priority to ARP080100032 priority patent/AR064750A1/es
Publication of EP1946829A1 publication Critical patent/EP1946829A1/fr
Withdrawn legal-status Critical Current

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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/02—Pretreatment of the raw materials by chemical or physical means
    • D21B1/026—Separating fibrous materials from waste
    • D21B1/028—Separating fibrous materials from waste by dry methods
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B9/00—General arrangement of separating plant, e.g. flow sheets
    • B03B9/06—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/46—Solid fuels essentially based on materials of non-mineral origin on sewage, house, or town refuse
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00141—Coils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/0084—Stationary elements inside the bed, e.g. baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00081—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00083—Coils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00085—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements
    • B01J2219/00135—Electric resistance heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00155—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00761—Details of the reactor
    • B01J2219/00763—Baffles
    • B01J2219/00765—Baffles attached to the reactor wall
    • B01J2219/00768—Baffles attached to the reactor wall vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00761—Details of the reactor
    • B01J2219/00763—Baffles
    • B01J2219/00765—Baffles attached to the reactor wall
    • B01J2219/0077—Baffles attached to the reactor wall inclined
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00761—Details of the reactor
    • B01J2219/00763—Baffles
    • B01J2219/00765—Baffles attached to the reactor wall
    • B01J2219/0077—Baffles attached to the reactor wall inclined
    • B01J2219/00772—Baffles attached to the reactor wall inclined in a helix
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00761—Details of the reactor
    • B01J2219/00763—Baffles
    • B01J2219/00765—Baffles attached to the reactor wall
    • B01J2219/00777—Baffles attached to the reactor wall horizontal
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C3/00—Other direct-contact heat-exchange apparatus
    • F28C3/005—Other direct-contact heat-exchange apparatus one heat-exchange medium being a solid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D1/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
    • F28D1/06—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with the heat-exchange conduits forming part of, or being attached to, the tank containing the body of fluid
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the invention relates to a process and apparatus for waste treatment.
  • Waste in particular municipal solid waste (MSW) and similar types of commercial waste, is an increasing burden on landfills and other forms of waste treatment. Part of the waste stream may be recycled through separated collection. Part of the landfill may be circumvented by incineration; however this is very costly and may have negative environmental impacts.
  • One of the alternatives suggested is treating the waste in an autoclave with steam while tumbling the content in order to breakdown the organic content and enable easier separation.
  • the organic fibres could be used as clean biomass fuel or compost; the glass/grit fraction - if sufficiently clean - can be used either by separating the glass for uses in recycled glass products, or it can be used as recycled aggregates.
  • the municipal waste does not have to be pre-selected, and is reduced to about 30 volume% of its original size. Further, when fibres are separated, and other useful materials are recycled, landfill can be limited to less than 10 volume% of the original waste.
  • the process to treat municipal solid waste comprises the steps of,
  • the vacuum applied in step (3) is about 0.5 bar (abs) or lower, and most preferably about 0.4 bar (abs) or lower.
  • the vacuum can be about 0.2 bar (abs) or higher, and may be about 0.3 bar (abs) or higher.
  • Another advantage of using a vacuum pump is that in depressurizing the vessel, time is gained (each batch will have a shorter cycle time in comparison to simply letting pressure off to atmaspheric), and even more importantly, that when opening the vessel after the autoclave treatment, no live steam is emitted and vapours displaced during emptying the autoclave contain only extremely small concentrations of Volatile Organic Compounds.
  • Any type of vacuum pump can be used if of sufficient capacity. More suitable vacuum pumps are eccentric-rotary vacuum pumps, which are preferred over positive displacement pumps. Suitable examples of a suitable type of vacuum pump include but are not limited to liquid-ring vacuum pump, rotary lobe pump and rotary gear pump. A liquid ring vacuum pump is preferred, as the water itself with rotor blades is acting as rotor. This is in particular an advantage as the gas stream from the scrubber still has some steam or water vapour. A liquid-ring vacuum can handle any additional water through an overflow to the central process-water system.
  • the vacuum pump has a capacity of about 1 m 3 /min or higher, more preferably about 2 m 3 /min or higher, as to allow sufficient vacuum to be reached in about 15 min or lower from the vessel, preferably about 10 min or lower, such as for example about 5 min.
  • the capacity will be about 50 m 3 /min or less, and preferably 30 m 3 /min or less, as a very large vacuum pump may be more expensive.
  • the upper limit is merely dictated by economical considerations. The lower limit has distinct additional technical effect in the speed of breaking up fibre due to vacuum expansion.
  • the capacity of the pump(s) is sufficient to achieve a vacuum of a certain vessel of 0.5 bar (abs) or less in 5 to 15 min, preferably 5-10 min when starting from 1 bar (abs).
  • the vacuum pump has a capacity sufficient to reach a vacuum of 0.5 bar (abs) in a vessel of about 10 cubic meter or more in about 15 min or less.
  • the gas may comprise steam, volatile organic compounds (VOC's) and dust.
  • VOC's volatile organic compounds
  • the scrubber steam is condensed, increasing the extraction rate of steam and/or air from the vessel.
  • the fluid to clean the exhaust gas is water. More preferably, the water is process water that is recycled in the system. This is an advantage, as much of the dust and volatile components may be kept in the waste treating cycles, and may be broken down in a next cycle.
  • the process water can be used to wet the MSW material, and to produce steam within the vessel. There is no need to use boiler quality feed water for these purposes.
  • the prior art suggests to use an eductor for this step, which appears to have the disadvantage of the need to use large amounts of fluid at substantial pressure to achieve a suitable vacuum in the desired time.
  • a suitable eductor would need to pump more than 1000 cubic metres per hour. Therefore, also the amount of energy required is much higher, which is a clear disadvantage.
  • the scrubber of the present invention only needs a pump capacity of about 50 cubic metres per hour and at lower pressure to be effective.
  • two or more vessels are used in an alternating fashion, while using the heat and steam from the discharge of step (3) to apply heat and/or steam to another vessel in a step (2').
  • This is also an advantage for efficient use of the vacuum pumps, as one pump or set of pumps can be used intermittently for the different vessels. Hence, only one pump or set of pumps is needed for processing with two or more vessels. It is preferred to have two or more pumps, in case the one needs maintenance, it is still possible to operate the plant.
  • the process comprises further a step of applying a vacuum after charging of the vessel, but before adding steam thereto.
  • a vacuum after charging of the vessel, but before adding steam thereto.
  • This has as advantage that pressure is more effectively increased to obtain a fully saturated environment. It furthermore has as advantage that the air displaced by the vacuum pump - which does comprise VOC's - is effectively cleaned in the scrubber.
  • Prior art suggests to add steam during loading to displace air. This has as a disadvantage that a large contaminated air/steam stream is emitted to the environment, or has to be handled.
  • the process to treat municipal solid waste in two or more vessels, which are used in an alternating fashion comprises the steps of,
  • the compressor may be a mechanically driven compressor (generally using electricity as energy source), but preferably would be a steam powered compressor.
  • steam powered or driven compressors it is suitable to use a steam ejector, steam eductor or steam driven jet pump. In the present application, these variants are together denoted as thermo-compressor.
  • the compressor is preferably a thermo-compressor, driven by steam of e.g. 6-15 bar gauge, which steam is supplied to the vessel.
  • This is in particular an advantage in case fresh steam is used to charge steam to the vessels. Adding fresh steam has the advantage of shortening the cycle-time. With shortening the cycle-time, the capacity of a.plant is increased.
  • the process to treat municipal solid waste in two or more vessels, which are used in an alternating fashion comprises the steps of,
  • the secondary circuits comprise a cooling element to lower the temperature of the thermal fluid, This may be important, as the inner surface of the vessel and the coils in the vessel preferably are about 100 °C or lower during unloading, and preferably during the time the vessel is at atmospheric pressure or lower, as otherwise plastic may stick to the walls of the vessel.
  • indirect heating with the thermal fluid is applied as soon as the vessel is charged with waste, and the door is closed.
  • the thermal fluid can be heated to a temperature of about 160 °C or higher, preferably of about 180 °C or higher, and even more preferred, about 200 °C or higher, such as for example up to about 250 °C. Higher temperatures are feasible, but may become expensive as special measures often have to be taken. Generally, the temperature of the thermal fluid is about 350 °C or lower. In view of the potential decomposition of plastics; it is preferred to keep the temperature of the thermal fluid at about 250 °C or lower.
  • thermal fluid mineral oils or synthetic fluids are suitable. Synthetic fluids are preferred due to their lower flashpoint and higher auto-ignition temperatures.
  • the heating is achieved by heating thermal fluid in the first circuit by for example direct fired heating coils containing the thermal fluid, or by electrical heating or the like.
  • the indirect heating of the autoclave vessel is done at least in part through a heated jacket.
  • heating is done through both conduits in the vessel, and a heated jacket which shortens the cycle time.
  • the process allows independent closure of the heating lines to either the jacket or the internal conduits.
  • Heating the jacket of the vessel has the advantage of increasing the heat transfer capacity which shortens the cycle time, and the heat transfer may be aided by having a flow of heating medium in the jacketed section of the vessel guided with internal baffles to ensure efficient heat transfer from the thermal fluid to the inside and contents of the vessel, as shown in the figure below.
  • it is advantageous to optimize this indirect heat transfer.
  • boiler steam can be strongly reduced, or even eliminated.
  • heating the contents of the autoclave is started as soon as the door is closed.
  • the total thermal energy input (steam and thermal fluid supplied by heating elements) per tonne of input municipal waste can be as low as 100 kWh, while achieving separated waste that has low inorganic in the biomass (or fibrous) fraction.
  • the average thermal energy input is about 125 kWh per tonne, while achieving a fibrous fraction with about 5 wt% or less that is non-biomass.
  • the non-biomass will be mainly grit and glass and small plastics.
  • the amount of non-biomass in the fibre is about 3 wt% or less, and most preferred about 1 wt% or less.
  • the amount of biomass in the non-fibre part preferably is - with a process requiring on average about 125 kWh or less energy input per tonne - preferably about 5 wt% or less, more preferably about 3 wt% or less, and even more preferred, about 1 wt% or less.
  • the average total energy input preferably is about 125 kWh per tonne or lower,
  • the amount of energy supplied through boiler steam is 25 % or less, relative to the amount of energy supplied by the thermal fluid system, more preferred the amount of fresh steam is about 10% or less relative to the average energy input. It is most preferred to have virtually no additional steam input in normal operation. This has a distinct advantage, that only a relatively small 'occasional-use steam boiler' is necessary which is only used e.g. in the start-up phase of the plant, or when uncommon process circumstances arise. This is an advantage, as the routine use of boiler steam causes a variety of process management issues, such as requiring 'clean' water feed, requiring softening of water (by added chemicals), requiring skilled operation for stability of steam production etc. Hence, it is preferred that about 90% or more of the average energy input per tonne of treated waste is supplied by the indirect heating system, and more preferably about 95% or more. To use virtually no steam during normal production is most preferred.
  • the steam boiler for occasional use is integrated in the thermal fluid heater. This has the advantage that only one heating apparatus is necessary for all energy input in the vessels even if direct and indirect heating is combined.
  • the complete plant including all apparatus to treat the waste material is enclosed in a building that is kept at a lower pressure than atmospheric pressure, and which further comprises a blo-filter for cleaning of ventilation air before discharge to atmosphere.
  • only the part of the waste treatment plant which receives the waste is kept under the lower than atmospheric pressure, and the extracted air from that part of the building is passed to atmosphere through a bio-filter.
  • the remainder of the plant being provided with local extract ventilation (LEV) hoods to preclude significant contamination of that part of the building's environment.
  • LEV hoods downstream of the autoclave has the further advantage that a safe environment for workers is achieved without the need for further protective measures.
  • extraction of dust and any remaining volatile material is sufficient to achieve a completely safe working environment.
  • the required under-pressure in a building housing the waste treatment facility, and/or the waste receiving part is achieved by applying about 1 or 2 or more air changes per hour via the building ventilation, thereby ensuring a flow of air into the building at all times.
  • the number of average air changes will be about 8 or less, and preferably, about 4 air changes will be sufficient.
  • the conveyors and other open separating equipment are fitted with LEV hoods to catch dust and volatile material (if present), the air streams so produced are passed to a scrubbing or cleaning section.
  • the hoods preferably are attached to the top of the conveyors, and are arranged to capture fugitive dust and VOC emissions via maintaining air in-flow at all openings to atmosphere around the conveyors. Openings are preferably about 5 cm or smaller, although 10 cm or smaller may occasionally occur. More preferably, openings are about 3 cm or smaller.
  • the air suction stream preferably maintains a velocity in the inward air streams through these openings of about 0.1 m/second or more and generally about 4 m/second or less.
  • the autoclave vessel when in an open position, has LEV hood elements nearby the opening, allowing suction of fumes and particles liberated during charging, and/or during discharging.
  • the suction-air velocity at the entrances to these LEV hoods is preferably about 0.3 m/second or more.
  • the LEV hood entrance air velocity can be 5 m/second or less.
  • the volumetric extraction capacity of these hood elements can be fairly low, as it is preferred not to add steam to the vessel during loading.
  • the scrubbing or cleaning section for treating the suction air may comprise filters that will need to be replaced or cleaned.
  • the waste-air stream is scrubbed with clean water to remove contaminants.
  • water can be discharged to waste-water treatment facilities, or can be further concentrated, and the organic fluid fraction can for example be used as organic feed in a sewage treatment digester plant.
  • the process comprises a classification step in which the majority of the fibre product, contaminated with small glass shards and grit particles, is subjected to an air separation step on a vibrating screen, which causes the lighter particles to flow downwards, and the heavier particles to move upwards.
  • the fibrous fraction that is to be classified is supplied to the middle section of the classification apparatus.
  • the apparatus comprises an inclined bottom screen through which an air stream flows.
  • the screen is vibrating, causing particles that lay on the screen to be transported upwards.
  • the air stream causes lighter particles to be lifted slightly above the screen, and thereby, the lighter particles flow over a kind of air cushion downwards.
  • the air velocity in such apparatus is relatively low in comparison to apparatus known as "air knives", and selected, in combination with the selection of tilt of the screen, and the strength of the vibration, to be sufficient to achieve an effective output, combined with an effective separation.
  • Glass particles may cause glass residue build-up in the combustion system, which may cause substantial maintenance problems. Further, also the inorganic material should be clean in the sense that preferably less than 3 vol%, and more preferably less than 1 vol%, is biomass waste in case this stream is to be used as a recycled aggregate for purposes such as road-fill.
  • One of the methods suggested in the prior art is the use of "air knives” to separate organic fibres from glass and grit. Air knife technology causes lighter material to float, and heavier material to fall down. It appeared that air knife technology is not suitable for good separation since both fractions remained highly contaminated.
  • (1) is the plant building that -in whole or in part - may be provided with suction apparatus to maintain ventilation extract to preclude fumes to escape from the building.
  • Air ventilation treatment may be provided through the use of bio-filters, preferably from the top of the building.
  • Waste is provided by vehicles into area (2). In this area, a manual or automated screening is performed by an operator to take away oversized waste like engine blocks, large pieces of concrete, carpets and the like. Preferably, this area has active air ventilation, preferably having 2-4 air changes per hour. Further, it is preferred to have the waste fed to a hopper (3), that is provided with a screen of e.g. 40-45 cm (18 inch) mesh to further preclude oversized parts in the autoclave.
  • the hopper is used to weigh the amount of waste fed to the autoclave.
  • the hopper may be equipped with a measurement of the weight and/or the volume to be put into the autoclave vessel.
  • a feed conveyer (4) is used to feed the autoclave.
  • the feed conveyer preferably is equipped with a spray nozzle (5) to wet the waste material.
  • the wetting agent preferably is contaminated process water (thereby usefully recycling this water) and preferably at elevated temperature (e.g. 30 to 80 °C).
  • the autoclave vessel (6) After the autoclave vessel (6) is charged, steam and/or heat is applied to the vessel.
  • the autoclave is first brought to reduced pressure, such as for example about 0.5 bar (abs) through the application of a vacuum system. Steam venting can be reduced in this way, as less air is to be replaced. Thereafter, steam is introduced, preferably from the other vessel, and the contents are vented for a short time (1-2 minutes).
  • the vacuum system can aid in achieving fast transfer of vented gasses, and contaminated air or steam can be cleaned in a scrubber. Thereafter, the vent of the autoclave is closed, and further steam and/or indirect heating is applied.
  • the content of the vessel is mixed, preferably through rotating the vessel.
  • the steam and temperature conditions should be chosen such that the content of the vessel is sterilized, and broken into small pieces.
  • Preferred process conditions are exemplified below.
  • General process conditions are a temperature above 121 °C, preferably above 130 °C. Generally, the temperature will be below 170 °C, as otherwise PVC will start to decompose. Preferably, the temperature will be below 160 °C.
  • the content is brought to atmospheric pressure and discharged on a conveyer (7), which transports the content to the down-stream classification area. It is preferred to dry the content in the autoclave through applying reduced pressure (to e.g. about 0.5 bar (abs)) and by applying indirect heating. It is preferred to transport the content into an intermediate hopper (8) in order to achieve fast discharge of the autoclave vessel.
  • the intermediate hopper (8) thereafter supplies the downstream classification area through conveyer (9).
  • the classification device may comprise suitable picking apparatus to discharge e.g. rags, which may be added to conveyer (9). Furthermore, it may be useful to have a large size screen (e.g. 14-30 cm (6-12 inch) screen) to remove large items before entering the classification section.
  • trommel screen 10
  • Other screening devices may be suitable as well.
  • a trommel screening device (10) or other device can have a plurality of classification sizes.
  • the lowest size fraction is about 12 mm or lower, although a size of about 10 mm or lower is preferred, and a size of about 8 mm or lower is even more preferred.
  • This fraction is transported via conveyer (11) to air classifier (12).
  • the next fraction (large particle fraction) will be generally about 50 mm or less, and may be about 40 mm or less.
  • This fraction may be transported via conveyer (13) to hopper (14). This will leave the oversize fraction of 4 or 5 cm or more, which can be transported over conveyer (15) to picking belt (16). On the picking belt, it is possible to remove plastic bottles, which are now clean and all labels are removed. Large wooden parts and other items may be collected.
  • Both the large particle fraction, as the over-sized fraction can be subjected to magnetic and Eddy current screening devices (depicted as 17) in order to remove iron, aluminum and other metals, batteries and the like. It may be suitable, to first have certain items picked from the picking belt, before collecting metals.
  • the low size fraction preferably is subjected to a further classification step in order to remove grit and glass shatters in classifier (12), which will give heavies (18), that may be combined with the larger fraction in (14), and which gives fibres (19).
  • the fibre fraction may be further treated to produce pellets or briquettes, or it can be used in loose form.
  • vessels 6 and 6' are the autoclaves. It will be understood by the skilled man, that two or more vessels are preferred, but that the vacuum system could advantageously be used in single vessel plants.
  • the autoclaves are equipped with vent openings (20) and (20') that are preferably located in or near the doors of the vessels. Each vent opening can be closed using manifolds (21) and (21').
  • the vents are connected to the vent line (22).
  • the vent line (22) can be used to evacuate one of the vessels, e.g. vessel (6), if valve (23) and (21) are open.
  • the contaminated air stream from the vessel is cooled and scrubbed in a scrubber (24) with water from the water tank (25) through line (26) with a pump if necessary (not shown).
  • the vacuum pump 27 allows air to be emitted through an entrainment separator (28), the effluent water being supplied via line (29) to the water tank (25). Vent air from entrainment separator (28) passes into the LEV extraction system for the building wherein this air could be further washed using clean water, filtered or otherwise treated alongside the contaminated air streams, e.g. arising from hoods and other places.
  • Water in the water tank (25) can be used to pre-wet the food to the autoclave through line (30), to feed the steam generator (31) through line (32).
  • boiler steam can be applied to vessel (6) after vessel (6) has been evacuated.
  • valve or manifold (20') of vessel (6') can be opened to line (33), while opening valve (34).
  • the supply of the steam can be aided by the use of a thermocompressor (35) or other means through line (36) to vessel (6) by opening valve (37).
  • the vent line of vessel (6) can be kept open for a few minutes to thoroughly ensure all residual air in vessel (6) is removed and a homogeneous steam atmosphere is achieved. Then, the valve (20) will be closed, and further steam (if necessary) can be added to vessel (6) from the boiler (31), after closing valve (34).
  • FIG. 3 shows an embodiment of a thermal fluid system, in which (6) and (6') denote the autoclave vessels.
  • the vessels are equipped with coils and/or a heating jacket to indirectly heat the content of the vessel.
  • a liquid thermal fluid is used as the heat transfer medium.
  • a primary circuit is depicted by line (40), that further comprises one heating element (41).
  • the heating element may be a burner, an electrical heated heat exchange element or the like.
  • the thermal fluid is preferably constantly pumped around primary distribution line (40) by pump (42).
  • pump (46) is started and valve (44) can be opened whereby hot thermal fluid is admitted into the secondary heating loop on vessel (6) and heating may commence.
  • valve (43) can be in whole or part, closed to direct the whole of the flow in the primary circuit to the secondary circuits and hence to maximize vessel heating.
  • valve (44) may be closed and valve (43) opened further to ensure thermal fluid heater (41) has sufficient flow to prevent overheating.
  • a cooler like for example a heat exchanger (45), or a blown air cooler, to cool the thermal fluid, and to preclude fouling of the heat internal transfer surfaces e.g. by adherence of melted plastic.
  • FIGs 4 and 4A show schematic drawings of a vessel which can be used by preference in the present process:
  • the vessel (6) is equipped with steam inlet pipes (50), and thermal fluid conduits (51) and (52).
  • the steam inlet pipes, and the thermal fluid conduits can be welded to the vessel as shown in Fig 4A .
  • the vessel preferably comprises a protective screen (53) at the bottom, and a door-opening (54).
  • the door (55) preferably has a vent opening (20), that is sealable through valve (21).
  • the conduits in the vessel it is possible to use one or more of the conduits in the vessel as vent pipes. In such a case, it is preferred that the conduit has its opening near the end of the vessel where the door is located.
  • Figure 4 shows the thermal oil conduits (52) to/from the jacket of the vessel, the jacket is fitted with circumferential baffle plates, that ensure high flow of the thermal fluid to all parts of the jacket and hence to all parts of the vessel shell whereby good heat transfer and effectiveness of the jacket to vessel heat transfer surface is assured.
  • the outside of the vessel insulated (56) e.g, from e.g. mineral wool insulation or foamed glass fibre, both for heat conservation, and for safety.
  • the steam inlet/vent outlets and oil conduits are preferably welded on top of each other, as to make baffles to push the material and make it tumble.
  • the baffles are adapted to be helical in the vessel longitudinal axis so as to be able to move material back and forth, depending on the direction of rotation of the vessel.
  • the vessel designed such that about 35% or more, preferably about 40% or more, and about 50% or less of the heat is transferred through the jacket. It is preferred, that about 65% or less, and about 50% or more of the heating energy is supplied through the internal conduits. This design allows relatively short cycle times per batch of treated waste, preferably using steam from another vessel as the only steam source.
  • Figure 5 shows a type of air classifier which appeared to be very suitable to achieve high purity organic fibre.
  • the classifier is equipped with a tilted plate (60) with perforations (61). Air (62) is blown through the perforations (61) by means of compressor (63).
  • the plate (60) is a vibrating plate, causing heavier particles (64) to shift upwards, while the air flow (which needs to be as low as convenient) causes the lighter particle (65) to flow on an air-cushion downwards.
  • Conveyers (18) and (19) can be used to transport the classified particles to hoppers, bunkers or other suitable place.
  • the classifier is equipped with a hood (66) to catch any dust that is blown out of the apparatus.
  • the hood preferably causes the contaminated air (67) to be transported to a dust collection device preferably a cyclone separator or filter (not shown).
  • the invention relates to a process to make a biomass fibre based fuel comprising the steps of
  • Drying the fibrous fraction in the autoclave by the application of heat and preferably also vacuum has the advantage that screening is more efficient. Fibres with a moisture content of more than 60%, e.g. 65% which is normal for non-dried steam treated fibers, are much more difficult to separate. Further, drying under vacuum has the advantage, that fibres are further subjected to break up by expanding moisture during drying and thereby the fibres lose integrity. This is also more advantageous than drying afterwards, as such a drying step will be at atmospheric pressure and less effective.
  • the content of the vessel is dried to have a fibrous fraction with a moisture content of about 55% or lower, and even more preferably about 50% or lower.
  • the fibrous fraction constitutes about 90 % or more of the theoretical achievable amount of biomass fraction. It actually appears possible to achieve a yield of fibrous fraction being about 95% or more of the original biomass, such as for example about 98%.
  • the amount of plastic in the fibre fraction is about 2% or less, more preferably about 1% or less. This is an advantage, as the use of the fibres as a biomass fuel qualifying for ROCs requires that >90% of the fuel energy content is from a renewable source. Plastic has a high calorific content, so only a very small amount is allowable in fibre to be used as a renewable biomass fuel.
  • the fibrous fraction after classification generally will have a moisture content of about 45% or lower. Depending on the end-use, the moisture content may be further lowered in a circulating flash dryer, a fluidized bed dryer, band dryer or the like.
  • the fibrous fraction may be pelletized, converted into briquettes for fuel and the like.
  • the fibrous fraction preferably has a low heavy metal content, such as for example less than 1 ppm Arsenic, and ⁇ 50 ppb Lead.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
EP07000166A 2007-01-05 2007-01-05 Procédé et appareil pour le traitement des déchets Withdrawn EP1946829A1 (fr)

Priority Applications (13)

Application Number Priority Date Filing Date Title
EP07000166A EP1946829A1 (fr) 2007-01-05 2007-01-05 Procédé et appareil pour le traitement des déchets
TW96149627A TW200918192A (en) 2007-01-05 2007-12-24 Process and apparatus for waste treatment
US12/522,191 US20100160709A1 (en) 2007-01-05 2008-01-01 Process and appratus for waste treatment
GB0902385A GB2456074B (en) 2007-01-05 2008-01-03 Process and apparatus for waste treatment
GB0800071A GB2445466B (en) 2007-01-05 2008-01-03 Process and apparatus for waste treatment
GB0800073A GB2445467B (en) 2007-01-05 2008-01-03 Process and apparatus for waste treatment
PCT/EP2008/050041 WO2008081028A2 (fr) 2007-01-05 2008-01-03 Procédé et dispositif de traitement de déchets
CL2008000013A CL2008000013A1 (es) 2007-01-05 2008-01-03 Procesos y aparatos para tratar los residuos solidos urbanos que comprenden un tratamiento con vapor de aire residual, calentamiento indirecto con fluido termico, transferencia de vapor forzado, diseno de autoclave, tratamiento residual de aire conta
GB0800074A GB2445468B (en) 2007-01-05 2008-01-03 Process and apparatus for waste treatment
EP20080701223 EP2107935A2 (fr) 2007-01-05 2008-01-03 Procédé et appareil pour le traitement des déchets
GB0800045A GB2445465B (en) 2007-01-05 2008-01-03 Process for waste treatment
GB0800072A GB2448390A (en) 2007-01-05 2008-01-03 Process and apparatus for waste treatment
ARP080100032 AR064750A1 (es) 2007-01-05 2008-01-04 Procedimiento y aparato para el tratamiento de residuos

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Cited By (6)

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WO2009069161A1 (fr) * 2007-11-29 2009-06-04 Energy & Ecology S.R.L. Procédé de dépolymérisation thermocatalytique de matière plastique
US7968057B2 (en) 2004-11-23 2011-06-28 Estech Europe Limited Autoclave
CN102500598A (zh) * 2011-10-27 2012-06-20 中国科学院广州能源研究所 一种生活垃圾高效分选提取可发酵有机物的方法和装置
CN106999997A (zh) * 2014-11-19 2017-08-01 皮尔斯·奥卡内 由废弃物生产堆肥、能源和燃料的先进生产技术
CN109351753A (zh) * 2018-10-27 2019-02-19 河南教育学院 一种废弃线路板中玻璃纤维的回收方法
CN115845779A (zh) * 2023-02-06 2023-03-28 河北新欣园能源股份有限公司 一种多功能化工生产用反应釜

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US4072273A (en) * 1974-01-07 1978-02-07 Southeast Sbic, Inc. Process for dry recovery of materials from solid refuse
US5190226A (en) * 1991-04-29 1993-03-02 Holloway Clifford C Apparatus and method for separation, recovery, and recycling municipal solid waste and the like
EP0633110A1 (fr) * 1993-07-02 1995-01-11 Phoenix Fibreglass Inc. Procédé pour la séparation des fibres des matériaux renforcés
US5387267A (en) * 1993-08-25 1995-02-07 Modular Energy Corporation Process and apparatus for treating heterogeneous waste to provide a homogeneous fuel
WO1995013148A1 (fr) * 1993-11-10 1995-05-18 Joseph Anderson Appareil, systeme et procede de traitement de matieres a recycler telles que des dechets.
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US6244199B1 (en) * 1996-10-22 2001-06-12 Traidec S.A. Plant for thermolysis and energetic upgrading of waste products
US6306248B1 (en) * 1997-11-20 2001-10-23 The University Of Alabama In Huntsville Method for transforming diverse pulp and paper products into a homogenous cellulosic feedstock
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7968057B2 (en) 2004-11-23 2011-06-28 Estech Europe Limited Autoclave
WO2009069161A1 (fr) * 2007-11-29 2009-06-04 Energy & Ecology S.R.L. Procédé de dépolymérisation thermocatalytique de matière plastique
CN102500598A (zh) * 2011-10-27 2012-06-20 中国科学院广州能源研究所 一种生活垃圾高效分选提取可发酵有机物的方法和装置
CN102500598B (zh) * 2011-10-27 2013-07-31 中国科学院广州能源研究所 一种生活垃圾高效分选提取可发酵有机物的方法和装置
CN106999997A (zh) * 2014-11-19 2017-08-01 皮尔斯·奥卡内 由废弃物生产堆肥、能源和燃料的先进生产技术
CN109351753A (zh) * 2018-10-27 2019-02-19 河南教育学院 一种废弃线路板中玻璃纤维的回收方法
CN115845779A (zh) * 2023-02-06 2023-03-28 河北新欣园能源股份有限公司 一种多功能化工生产用反应釜
CN115845779B (zh) * 2023-02-06 2023-05-16 河北新欣园能源股份有限公司 一种多功能化工生产用反应釜

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